US20010049330A1 - Preparation of catalysts useful in the preparation of phenol and its derivatives - Google Patents

Preparation of catalysts useful in the preparation of phenol and its derivatives Download PDF

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Publication number
US20010049330A1
US20010049330A1 US09/682,010 US68201001A US2001049330A1 US 20010049330 A1 US20010049330 A1 US 20010049330A1 US 68201001 A US68201001 A US 68201001A US 2001049330 A1 US2001049330 A1 US 2001049330A1
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Prior art keywords
zeolite
benzene
catalyst
phenol
process according
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US09/682,010
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English (en)
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Leonid Kustov
Viktor Bogdan
Vladimir Kazansky
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Priority claimed from RU97112675A external-priority patent/RU2127721C1/ru
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/60—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by oxidation reactions introducing directly hydroxy groups on a =CH-group belonging to a six-membered aromatic ring with the aid of other oxidants than molecular oxygen or their mixtures with molecular oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/26—After treatment, characterised by the effect to be obtained to stabilize the total catalyst structure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/36—Steaming
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • This invention is related to the field of organic synthesis, and in particular, to the methods for preparing hydroxylated aromatic compounds (e.g., phenol and its derivatives), by selective oxidation of aromatic compounds (e.g., benzene and its derivatives), with gaseous mixtures comprising nitrous oxide in the presence of heterogeneous catalysts.
  • hydroxylated aromatic compounds e.g., phenol and its derivatives
  • aromatic compounds e.g., benzene and its derivatives
  • gaseous mixtures comprising nitrous oxide
  • heterogeneous catalysts Commercial zeolites or zeolite-containing catalysts modified by special treatments described herein are used as heterogeneous catalysts.
  • phenol and its derivatives such as diphenols, chlorophenols, fluorophenols, alkylphenols and the like.
  • Known processes include direct oxidation of aromatic hydrocarbons or their derivatives with O 2 , N 2 O or other gaseous oxidants in the presence of oxide catalysts such as those referenced in U.S. Pat. No. 5,110,995.
  • oxide catalysts such as those referenced in U.S. Pat. No. 5,110,995.
  • oxide catalysts for the direct oxidation of benzene to phenol in the presence of molecular oxygen do not provide high selectivity and yield of the target product.
  • the most successful example of such a catalyst is prepared from phosphates of various metals.
  • ZnPO 4 has been used as a catalyst for benzene oxidation into phenol in the presence of alcohols. At temperatures of 550-600° C., the ZnPO 4 catalyst produced a phenol yield of about 25%. However, the selectivity of ZnPO 4 was poor (60%) [Japan Patent No. 56-77234 and 56-87527, 1981]. Furthermore, phosphate catalysts are disadvantageous for benzene oxidation because they consume substantial quantities of alcohols.
  • Vanadium-, molybdenum-, or tungsten-based oxide catalyst systems for direct benzene oxidation with nitrous oxide (N 2 O) at 500-600° C. are known [Iwamoto et al., J. Phys. Chem., 1983, v. 87, no. 6, p. 903].
  • the maximum phenol yield for such catalysts in the presence of an excess of steam is about 7-8%, with a selectivity of 70-72%.
  • the main drawbacks of these catalysts are their low selectivity and yield of phenol, the required high temperatures for the reaction, and the requirement to add steam.
  • Zeolite catalysts are also available for the selective oxidation of benzene and its derivatives using N 2 O as an oxidant (E. Suzuki, K. Nakashiro, Y. Ono, Chem. Lett., 1988, no. 6, p. 953-1 M. Gubelmann et al., Eur. Pat., 341, 165, 1989-1 M. Gubelmann et al., U.S. Pat. No. 5,001,280, 1990).
  • high-silica ZSM-5 type pentasil zeolites are used as catalysts for oxidation of benzene, chlorobenzene, and fluorobenzene into corresponding phenols.
  • the zeolites of the pentasil type e.g., ZSM-5, ZSM-11, ZSM-12, ZSM-23
  • mordenite e.g., zeolites of the pentasil type
  • zeolite Beta e.g., mordenite
  • zeolite Beta e.g., zeolites of the pentasil type
  • mordenite e.g., mordenite
  • zeolite Beta and EU-1 which are all modified with small iron additives during their synthesis
  • the disadvantages of these catalysts include the necessity to introduce iron ions into the zeolite and to control the oxidation state of iron ions, the low liquid space velocity value of benzene, the significant contact time necessary to obtain acceptable, but not impressive yields of the final product, and the low selectivity at elevated temperatures ( ⁇ 450° C.).
  • phenol is produced by oxidative hydroxylation of benzene and its derivatives with nitrous oxide at 225-450° C. in the presence of an iron-containing zeolite catalyst.
  • This zeolite catalyst is pretreated at 350-950° C. in steam containing 0.1-100 mol. % H 2 O (Kharitonov A. S., et al., U.S. Pat. No. 5,672,777, 1997—Russian Patent No. 2074164, C07C 37/60, Jun. 1, 1997 application No. 94013071/04, C07C 37/60, 27.12.1995).
  • treatment of the zeolite catalyst using this method does not cause a substantial increase in the activity.
  • Another drawback of this method is the low stability of the resultant catalyst, which deactivates during the oxidation process due to the formation of tar-like side-products.
  • Another disadvantage of all the methods described above is the low partial pressures of benzene in the vapor mixture—the benzene content was 5 mol. % and the partial pressure of benzene was about 40 torr.
  • an object of the present invention is to develop a method of preparing hydroxylated aromatic compounds (e.g., phenol and derivatives) by selective oxidation of aromatic compounds (e.g., benzene and its derivatives).
  • N 2 O as a mild oxidant in the presence of an appropriate catalyst that enhances productivity of the oxidation process by increasing the yield of hydroxylated aromatics and selectivity for the target product.
  • the objects of the invention are accomplished by a method of preparing hydroxylated aromatic compounds (e.g., phenol or its derivatives) by oxidation of aromatic compounds (e.g., benzene and derivatives) with nitrous oxide.
  • the method of the present invention significantly increases the process efficiency due to the increase in the activity and selectivity of the catalyst, and the increase in the yield of the target products (i.e., hydroxylated aromatic compounds).
  • the aromatic compounds are oxidized using nitrous oxide at 225-500° C. in the presence of a zeolite catalyst.
  • the zeolite catalyst according to the invention is modified with strong Lewis acid-base sites of a specific nature. These sites can be introduced into the zeolite catalyst by performing a special high-temperature pretreatment. This preliminary thermal activation of the H-form of zeolite is carried out in two steps. In the first step, the catalyst is heated at 350-450° C. for 4-6 h in an inert gas (nitrogen or helium) or air stream. In the second step, the catalyst is calcined at 450-1000° C.
  • the hydroxylated aromatic compounds are phenol and its derivatives, and the aromatic compounds are benzene and its derivatives.
  • the purpose of the two-step high-temperature treatment is related to the generation of a specific type of Lewis acid-base pair centers, preferably framework Lewis acid-base sites. This is achieved by separating the stage of removal of adsorbed water and/or ammonium ions (which are introduced via ion exchange at the stage of the preparation of an H— or NH 4 — forms of zeolites), from the stage of removing structural (bridging) OH groups intrinsic to the H-zeolite framework. For this purpose, the thermal treatment is carried out in two steps.
  • the zeolite is calcined at a temperature up to 350-450° C. (a conventional pretreatment). In this first step, adsorbed water and exchanged ammonium ions are intensively removed.
  • the zeolite is calcined at temperatures ranging from 450 to 950° C., depending on the zeolite composition. In this second step, structural (acidic) OH groups of zeolites are removed.
  • This second step can solve two problems: (1) removing acidic OH groups that are the active sites for side reactions leading to the formation of tar-like products; and (2) creating new (aprotic) rather strong Lewis acid-base pairs, preferably related to the framework of the zeolite, that are capable of activating N 2 O molecules to cause evolution of molecular nitrogen and formation of atomic oxygen species adsorbed on strong Lewis acid sites.
  • the atomic oxygen acts as a mild oxidizing agent in the reaction of selective oxidation of aromatic compounds to corresponding hydroxylated aromatic compounds.
  • the strong Lewis acid-base centers as precursors of the active oxidizing centers (atomic oxygen) can be detected by IR spectroscopy using adsorbed probe-molecules, such as CO, H 2 , CH 4 , etc.
  • the starting materials for the preparation of the zeolite catalysts are the commercial forms of zeolites, such as:
  • a commercial ZSM type zeolite ZSMe-5, ZSM-11, ZSM-12, ZSM-23 etc.
  • the Si/Al or Si/Me ratio ranges from 40 to 100.
  • the commercial zeolite is acidified by addition thereto of an inorganic or organic acid.
  • the zeolite is acidified by soaking it with from 10 ml to 100 ml of acid per gram of a zeolite, wherein the acid has a normality of from 0.1 N to 2 N.
  • the acid soaking may be done in a single step, or more preferably, in several steps.
  • Acid forms of zeolite may be also prepared by exchanging of a commercial zeolite with an aqueous solution of an ammonium salt (e.g., a nitrate or chloride salt).
  • an ammonium salt e.g., a nitrate or chloride salt
  • a Na-form of ZSM-type zeolite is treated with a 0.1-2 N solution of an appropriate ammonium salt.
  • the ion exchange degree of sodium for ammonium or protons is varied from 30 to 100%, and more preferably from 50 to 95%.
  • Zeolites can be used as catalysts in the pure form or in a combination with an appropriate binder.
  • amorphous silica with a specific surface area ranging from 100 to 600 m 2 /g, or alumina with a specific surface area ranging from 100 to 400 m 2 /g, or a mixture thereof are used as binders.
  • the content of the binder in the catalyst ranged from 5 to 50 wt %, and more preferably from 20 to 30 wt %.
  • Nitrous oxide may be employed alone, or in admixture with an inert gas such as nitrogen or helium, or in admixture with air.
  • Aromatic hydrocarbons such as benzene, toluene, ethylbenzene, cumene, xylenes and the like, the halogenated aromatic compounds such as chlorobenzene, fluorobenzene, difluorobenzenes and the like, phenol, styrene or a mixture thereof are typically used as substrates for selective oxidation with nitrous oxide. It is also possible to selectively further oxidize an aromatic compound such as phenol, using the process described herein. For purposes of this specification, these substrate materials will be generally referred to as “aromatic compounds.”
  • the substrate is typically introduced in a mixture with nitrous oxide in a molar ratio of nitrous oxide to substrate ranging from 1:7 to 5:1, and more preferably, from 1:2 to 4:1.
  • the LHSV of the substrate ranged from 0.2 to 5 h ⁇ 1 , more preferably from 0.5 to 2 h ⁇ 1 .
  • the reaction is preferably carried out at a temperature from 300 to 500° C., and more preferably from 350 to 450° C.
  • the contact time of the reaction mixture with a catalyst ranges from 0.5 to 8 sec, and more preferably from 1 to 4 s.
  • the gases evolved from the reactor may comprise a mixture of phenol and dihydroxybenzenes and are condensed and separated by any technique known to this art (GC, LC, MS or a combination thereof).
  • the catalyst can be easily and reversibly regenerated by calcination at 400-600° C. in a flow of air, oxygen, and nitrous oxide, or mixtures thereof with an inert gas. The regeneration is carried out for 1-3 h.
  • the catalyst was cooled down to the reaction temperature (i.e., 350° C.) in flowing nitrogen.
  • the reaction was carried out continuously by introducing a mixture of: benzene with a LHSV of 0.5-2 h ⁇ 1 nitrous oxide and helium (nitrogen).
  • the mixture's contact time was 1-4 sec.
  • Example 1 Conditions of high- Deactivation temperature treatment, (during ° C. C, % S, % Y, % 60 min), % 350 10 97 9.7 50 450 12 95 11.4 42 650 16 95 15.2 45 750 21 96 20.2 42 850 29 94 27.8 14 920 36 98 35.3 11 1100 0 — — —
  • the final temperature of the high temperature treatment was 900° C.
  • the catalyst was tested in benzene oxidation with N 2 O. In this test, the benzene LHSV was 1.7 h ⁇ 1 , the benzene-to-N 2 O molar ratio was 7:1 (a large excess of benzene over N 2 O), and the temperature was 440-470° C.
  • the yield of phenol (on the basis of N 2 O) was 20.6% at 440° C. and 30.2% at 470° C.
  • the efficiency of N 2 O utilization for selective oxidation of benzene to phenol was 95-96%.
  • a gallium-modified HZSM-5 zeolite was prepared by impregnation of a HZSM-5 zeolite with an aqueous solution of gallium nitrate, followed by calcination at 500° C. for 4 h to remove the nitrate ions (the Ga 2 O 3 content was 3 wt %).
  • the zeolite was subsequently pretreated at 850° C. and was loaded in the reactor. 2.3 g (particle size, 1-2 mm) of the zeolite was treated in this manner.
  • Benzene was supplied with a LHSV of 0.5 h ⁇ 1 at the N 2 O:C 6 H 6 ratio of 0.5:1.
  • the yield of phenol was 20.8% on the basis of N 2 O, or 10.4% on the basis of benzene.
  • the selectivity was 100%.
  • the efficiency of N 2 O utilization for selective oxidation of benzene to phenol was 100%.
  • Example 3 250 mg of 0.5-1.0 mm particle size catalyst was prepared according to Example 3. This catalyst was diluted with quartz grains (750 mg), and the mixture was loaded into the reactor. Benzene (Example 13) and phenol (Example 14) were used as substrates. The nitrous oxide: substrate ratio was 4:1, the LHSV was 0.5 h ⁇ 1 , and the reaction temperature 430° C. In the case of benzene, a product comprising 75% phenol and 25% of a mixture of o- and p-diphenols (in a 1:4 ratio) was obtained. The overall yield was 60%, and the selectivity was 97%. In the case of phenol, a mixture of o-, m-, and p-diphenols in the ratio 1.0:0.5:4.0 with the overall yield of 75% was produced.
  • the benzene conversion for the catalysts according to the invention may be increased from 10-20% to 50-75% without decreasing the selectivity ( ⁇ 98-100%);
  • the stability and the life time of a catalyst may be considerably improved by modifying a zeolite catalysts to introduce strong Lewis acid-base sites. These sites have a specific nature, and are created by high-temperature calcination of the zeolites preceding the catalytic testing;

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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US09/682,010 1997-07-05 2001-07-09 Preparation of catalysts useful in the preparation of phenol and its derivatives Abandoned US20010049330A1 (en)

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RU97112675 1997-07-05
RU97112675A RU2127721C1 (ru) 1997-07-29 1997-07-29 Способ получения фенола и его производных
US09/078,253 US6414197B1 (en) 1997-07-05 1998-05-13 Preparation of phenol and its derivatives
US09/682,010 US20010049330A1 (en) 1997-07-05 2001-07-09 Preparation of catalysts useful in the preparation of phenol and its derivatives

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BR (1) BR9805598A (enExample)
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11008276B2 (en) 2014-10-02 2021-05-18 Monsanto Technology Llc Processes for preparing 2,5-dichlorophenol
CN114478198A (zh) * 2022-01-27 2022-05-13 大连大学 一种催化加氢愈创木酚制备苯酚的方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2155181C1 (ru) 1999-04-05 2000-08-27 Кустов Леонид Модестович Способ окисления бензола и/или толуола в фенол и/или крезолы
DE10036953A1 (de) * 2000-07-28 2002-02-07 Bayer Ag Verfahren zur Herstellung von Hydroxyaromaten

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US4180693A (en) * 1976-10-15 1979-12-25 Institut Francais Du Petrole New preparation process of a catalyst for converting aromatic hydrocarbons
US4581214A (en) * 1984-01-17 1986-04-08 Union Oil Company Of California Shock calcined aluminosilicate zeolites
US5013700A (en) * 1986-11-14 1991-05-07 Lars Falth Method of producing dealuminized zeolite Y of high hydrophobicity
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US5348924A (en) * 1989-09-29 1994-09-20 Exxon Research & Engineering Co. Zeolite aggregates and catalysts
US5576256A (en) * 1994-05-23 1996-11-19 Intevep, S.A. Hydroprocessing scheme for production of premium isomerized light gasoline
US6110258A (en) * 1998-10-06 2000-08-29 Matheson Tri-Gas, Inc. Methods for removal of water from gases using superheated zeolites
US6180549B1 (en) * 1998-09-10 2001-01-30 The B. F. Goodrich Company Modified zeolites and methods of making thereof
US6395664B1 (en) * 1998-02-19 2002-05-28 Uop Llc Process for reactivating a deactivated dehydrocyclodimerization catalyst with water

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US3528615A (en) * 1967-06-16 1970-09-15 Mobil Oil Corp Method of reducing particle size of crystalline zeolites
US4016218A (en) * 1975-05-29 1977-04-05 Mobil Oil Corporation Alkylation in presence of thermally modified crystalline aluminosilicate catalyst
US4180693A (en) * 1976-10-15 1979-12-25 Institut Francais Du Petrole New preparation process of a catalyst for converting aromatic hydrocarbons
US4581214A (en) * 1984-01-17 1986-04-08 Union Oil Company Of California Shock calcined aluminosilicate zeolites
US5013700A (en) * 1986-11-14 1991-05-07 Lars Falth Method of producing dealuminized zeolite Y of high hydrophobicity
US5077026A (en) * 1987-03-02 1991-12-31 Georgia Tech Research Corporation Ferrisilicate molecular sieve
US5348924A (en) * 1989-09-29 1994-09-20 Exxon Research & Engineering Co. Zeolite aggregates and catalysts
US5576256A (en) * 1994-05-23 1996-11-19 Intevep, S.A. Hydroprocessing scheme for production of premium isomerized light gasoline
US6395664B1 (en) * 1998-02-19 2002-05-28 Uop Llc Process for reactivating a deactivated dehydrocyclodimerization catalyst with water
US6180549B1 (en) * 1998-09-10 2001-01-30 The B. F. Goodrich Company Modified zeolites and methods of making thereof
US6110258A (en) * 1998-10-06 2000-08-29 Matheson Tri-Gas, Inc. Methods for removal of water from gases using superheated zeolites

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11008276B2 (en) 2014-10-02 2021-05-18 Monsanto Technology Llc Processes for preparing 2,5-dichlorophenol
CN114478198A (zh) * 2022-01-27 2022-05-13 大连大学 一种催化加氢愈创木酚制备苯酚的方法

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JPH11171809A (ja) 1999-06-29
AU7393498A (en) 1999-01-14
AU753188B2 (en) 2002-10-10
EP0889018B1 (en) 2002-01-30
CA2240612A1 (en) 1999-01-29
DE69803634D1 (de) 2002-03-14
DE69803634T2 (de) 2002-09-12
EP0889018A1 (en) 1999-01-07
ES2169895T3 (es) 2002-07-16
TW513400B (en) 2002-12-11

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